glasgow



Feb. 21, 1956 c. o. GLASGOW 2,735,506

COMBINATION DEHYDRATOR-SEPARATORS FOR PETROLEUM WELL STREAMS Filed Sept. 29, 1954 6 Sheets-Sheet l Fig.

Fig.3

:INVENTOR $3; CIarence 0. Glasgow ATTORNEYS Feb. 21, 1956 I c. o. GLASGOW 2,735,506

COMBINATION DEHYDRATOR-SEPARATORS FOR PETROLEUM WELL STREAMS Filed Sept. 29, 1954 6 Sheets-Sheet 2 BY I 6 A TTORNEYS Feb. 21, 1956 c. o. GLASGOW 2,735,506

COMBINATION DEHYDRATOR-SEPARATORS FOR PETROLEUM WELL STREAMS 6 Sheets-Sheet 5 Filed Sept. 29, 1954 INVENTO'R C/arenca 0. G/asgow W2 ATTORNEYS Feb. 21, 1956 c. o. GLASGOW 2,735,506

COMBINATION DEHYDRATOR-SEPARATORS FOR PETROLEUM WELL STREAMS Filed Sept. 29, 1954 6 Sheets-Sheet 4 a Q Q Q *3 w 5, m L

INVENTOR Clarence 0. Glasgow ATTORNEYS Feb. 21, 1956 c. o. GLASGOW 2,735,506

COMBINATION DEHYDRATOR-SEPARATORS FOR PETROLEUM WELL STREAMS Filed Sept. 29, 1954 6 Sheets-Sheet 5 ATTORNEYS Feb. 21, 1956 c. o. GLASGOW COMBINATION DEHYDRATOR-SEPARATORS FOR PETROLEUM WELL STREAMS 6 Sheets-Sheet 6 Filed Sept. 29, 1954 IJIIIIIII INVENTOR Clarence 0. Glasgow BY WW ATTORNEYS United States Patent COMBINATION DEHYDRATOR-SEPARATORS on PETROLEUM WELL Clarence 0. Glasgow, Tulsa, Okla, assigno-r to National Tank Company, Tulsa, Okla, a corporation of Nevada Application September 22, 1954, Serial 1510. 459,928 Claims. or. 183 2.7)

This invention relates to new and useful improvements in combination dehydrator-separators for petroleum well Str ms The invention is particularly concerned with combination units in which a petroleum well stream is resolved into gaseous and liquid components, or into gaseous, water and oil components, and in which the separated gaseous phase is subjected to the action of a liquid desiccant for the removal of water vapor therefrom. ,The invention is also directed particularly to the provision of a unit of this character particularly adapted for'use in cold weather or cold climates wherein there is encountered a likelihood of freezing of the water separated from the well stream. a

It is, therefore, a principal object of the invention to provide an improved combination unit for effecting liquid-gas separation of a petroleum well stream and 'dehydration of the separated gaseous phase by means of a liquid desiccant, which is unitaryan'd compact in structure and affords the carrying out of these operations within a single vessel, as well as'the reconcentration of the liquid desiccant and the removal of water'therefrom to permit recirculation of said desiccant into contact with. the gaseous phase.

Another principal object of the invention is to provide an improved combination unit for effecting liquid-gas separation of a petroleum well stream and dehydration of the separated gaseous phase by means of a liquid desiccant, wherein provision is made for heating the liquid desiccant for reconcentration thereof and removal of water vapor therefrom, and in which there is established a novel and unique heat exchange relationship between the separator portion of the unit and the desiccant reconcentrating portion of the unit to provide the desired cooling of the reconcentrated desiccant and the supplying of heat to the separator section to prevent freezing of water therein as Well as to prevent congealing of any waxy material, distillate emulsions, or other material which may be present.

Other and more specific objects will be apparent from a reading of the following description of the construction and operation and various modifications of the invention. i

A construction designed to carry out the invention wlil be hereinafter described together with other features of the invention.

The invention will be more readily understood from a reading of the following specification and by reference to the accompanying drawings, wherein examples of the invention are shown, and wherein:

Fig. l is a vertical, longitudinal, sectional view of a combination unit constructed in accordance with this invention and adapted to carry out the separation of a petroleum well stream into water, oil or distillate, and gaseous components, accompanied fby the' subjection of the gaseous component to the action of a liquid desiccant and the continuous reconcentration and recirculation of the desiccant,

2,735,506 C6 Patented Feb. 21, 1956 Figs. 2 and 3 are vertical, cross-sectional views taken upon the respective lines of Fig. l,

Fig. 4 is a'vertical, longitudinal, sectional view of a modified form ofthe invention in which a liquid-gas separation of the' well stream is carried out followed by withdrawal of all"sepa'rated liquids througha common outlet, i

Fig. 5 and 6 are vertical, cross-sectional views taken on the respective lines of Fig. 4; Fig. 7 is an enlarged, horizontal, cross-sectional view taken uponthe line 7+7 of Fig. 1'; I

Fig. 8 is a plan view'of the modification shown in Fig. 1, the view showing the complete structure of the "assent y, 1

Fig. 9 is a side elevation of the complete unit of Fig. 1,- Fig. 10 is a vertical, cross-sectional view taken upon the line 10 10 of Fig. 9 and showing in essence 'anend elevation of the completeassembly of Fig. 'l,

Fig. 1.1 is an enlarged sectional view of the dilute desiccant-'reconcentrated desiccant heat exchanger,

Fig. 12 isan enlarged sectional view of one of the volume tanks,

Fig. 13 is a side elevation, partly broken away, of a further modification of the invention,

Fig. 14 is an end elevation, partly broken away, of the modification of Fig. 13, i

Fig. 15 is a plan view of the modification of Fig. 13, and

Figs. 16 and 17 are enlarged horizontal, transverse, sectional views takenupon the respective lines of Fig. 13.

In the drawings, the 'iiumeral'lll designates" an elongate, horizontal vessel enclosing a separator sectionA and a desiccant reconcentrator' section B. By reason of the pressures involved, the section A includes an elongatepcylindrical,relatively heavy-walled shell ,11 having its outer or outlet end'closedby a'dishedh'ea'd v12, and its inner or inlet end closed by a dished head 13. The reconcentrator section B compris'es an elongate, cylindrical, relatively thin-walled shell'14 having its outer" end closed ,by' a dished head ,15, and having its inner end joined to the head 13 of the vessel 11 whereby' the inner end of the shell' 14 is adequately sealed and closed, and whereby "the head 13 is caused to form "a partition in common between the sections A and B. flfhe'composite vessel 10 is carried upon suitable supports' 16' which'fin turn, as will appearmore fully hereinafter, may be carried upon a skid or other base element describedhere'im after. I

There is provided a petroleum well stream inletfitting .17 extending through the side wall of the section A near the inner head 13 thereof the inlet fitting commu nicating with the interior of'the section A' through a, box-like enclosure 18 having therein vertically disposed angular baflles or scrubbing members v19 which serve to trap and remove any large particles of liquid present inthe incoming gas stream. The well stre'am, thus denuded of liquid slugs or appreciably-sized bodies orparticles of liquid, passes intotheop'en interior of the section 11 and flows longitudinally thereof toward the outlet end of the section. Sinceithe velocity of how ofthe well stream is greatly reduced upon entering the separator section 'A, and since the well stream is caused to undergo horizontal ilow within the separator action, liquid particles present in the well stream promptly settle to the bottom of the separator section and are collected therein between the head .13 and a transverse baffle 20 extending upwardly from the lower 'wallof the shell 11 to a pointn'ear the axis thereof. Complete retention of separated liquid within the inlet portion of the separator section A isassured by a transverse partitionZl extending across the vessel ,llbetwe'en the battle 20 and the head 12at the outlet end of the vessel. liquidsaccurnulating within this inlet section will stratify, of course, into water and oil or distillate layers, the distillate layer being uppermost because of itsspecific gravity. The water layer will be retained between the bafileZGand the head 13 and will be drawn off from the vessel through the adjustable water leg structure 22 in accordance with the The oil or distillate rate at which the water accumulates. skims over the upper edge of the baffle 20 and is withdrawn from the space between the baflie 20 and the partition 21 through an outlet fitting 23, again, in accordance with the rate at which the distillate accumulates.

The portion of the vessel 11 between the partition 21 and the head 12 constitutes a dehydrator section C having an inlet 24 in its upper wall' for admission of liquid desiccant such as diethylene glycol, triethylene glycol, calcium chloride solution, or the like, for the removal of water vapor from the separated gaseous phase of the well stream. The liquid desiccant is flowed onto a transverse, horizontal, foraminous plate 25 supported within the shell 11 between the upper portions of a verti- A cal baffle 26 spaced closely to the partition 21, and a similar vertical bafiie 27 positioned substantially medially ,of the chamber CI Gas flowing upwardly through the maintain a constant level of liquid desiccant in the section C beneath the plate 25 and permit the excess desiccant to spill over the upper edge of the seal baffie 28 nearest the head 12 and flow from the vessel 11 through a desiccant outlet fitting 29. Of course, this liquid seal structure prevents the passage of gas under the baffle 27 and forces the gas to move upwardly through a mist extractor maze 30 and the perforated plate 25and pass over the upper edge of the bafile 27.

For transmitting the gaseous phase separated from the well stream from the separator section of the vessel to the dehydrator section, there is provided in the separator section a vertical gas outlet pipe 31having its open upper end adjacent the upper wall of the separator section and being connected through an elbow 32 to a spreader pipe 33 extending through the lower portion of the partition 21 and having its perforated lower wall 34 submerged in the body of desiccant retained in the dehydrator section by the seal baffles 28 and underlying the perforated plate 25. Thus, the gaseous portion or phase of the well stream, after separation of the liquid portion thereof, is conducted through the partition 21, with adequate provision for preventing the simultaneous passage of liquid, and passed in thorough scrubbing contact with a supply of liquid desiccant entering the dehydrator section C through the inlet fitting 24. After being subjected to the action of the liquid desiccant, the gas passes througha mist extractor 35 and leaves the vessel 11 through a gas outlet conductor 36.

As is well known, liquid desiccants function to dehydrate gas by reason of the difference in water vapor pressures between the desiccant and the gas, and hence, the desiccant absorbs water from the gas stream to an extent as to reduce its eflicacy. Therefore, it is desirable that the diluted desiccant be subjected to a heating step in order to drive oit excess moisture and to reconcentrate the desiccant for recycling and further use. Before reexposure of the desiccant to the gas stream, however,

it is important that the desiccantbe cooled from its reconcentrating temperature in order that its efliciency as a water absorbant may be increased. Further, in units of this type in which water is separated from a well stream and becomes subject to freezing by reason of 4 the separation and accumulation in a vessel exposed to winter temperatures or to cold climates, it is important that the accumulated body of water be maintained at a temperature sufiicient to prevent it from freezing and clogging the separating structure. The present invention accomplishes both of these desirable results by incorporating the reconcentrator section B and the separator section A into a common vessel having the common wall or partition 13.

The diluted or exhausted desiccant, upon leaving the vessel 11 through the outlet fitting 29 passes into an external volume tank 37 and flows therefrom through an outlet conductor 38 and a diaphragm operated valve 39 to a conductor 40 connected with a heat exchanger coil 41 disposed within a heat exchanger shell 42 positioned beneath the reconcentrator section B. The dilute desiccant is heated in its passage through the heat exchanger coil 41, and flows therefrom through a conductor 43 to the inlet 44 of a bubble column 45 extending upwardly from the reconcentrator section. The reconcentrated desiccant, having had water removed therefrom, leaves the reconcentrator section through an outlet fitting 46 and passes through the heat exchanger shell 42 in heat exchange with the coil 41 therein, and thereby delivers up a sizeable portion of its heat to the dilute desiccant passing through the coil 41. From the shell 42, the cooled and reconcentrated desiccant flows through a conductor 47 into a heat exchanger jacket 48 which surrounds an appreciable length of the conductor 40. The jacket 48 is of considerable length and thus affords a counter-current flowing of the concentrated and dilute desiccants through an elongate path for further and more complete heat exchange and transfer of heat from the reconcentrated desiccant to the dilute desiccant as preheat. V

Beneath the opposite or separator end of the unit 10, the cooled and reconcentrated desiccant leaves the heat exchange jacket 48 through a conductor 49 and passes to the inlet of a gas operated pump 50. The pump discharges the reconcentrated desiccant under pressure through a conductor 51 connected to the inlet of a heat exchange coil 52 disposed within the dehydration chamber C between the bafile 27 and the head 12 and immediately below the mist extractor 35. A final cooling of the desiccant is thus achieved by indirect heat exchange with the relativelycool gas passing from the section C, and this thoroughly cooled desiccant is conducted from the outlet 53 of the coil 52 through a conductor 54 connected to the desiccant inlet 24.

Within the reconcentrator section B the unit is provided with a return bend fire tube or heating unit 55 underlying the bubble column 45 and disposed adjacent the lower wall of the vessel 14. A transverse baffle or weir 56 extends upwardly from the lower wall of the vessel between the fire tube 55 and the head 13 and terminates closely adjacent the upper wall of the vessel. Thus, a considerable body of liquid is held in the vessel around and over the fire tube 55.

The dilute desiccant entering the column 45 through the inlet fitting 44 spills downwardly through the column in heat exchange with water and desiccant vapors arising therethrough, thus serving to condense a large portion of the desiccant vapors and, in turn,- being itself preheated with some vaporization of water. The downwardly flowing dilute desiccant stream is diverted near the bottom of the column 45 by means of a perforated partition 57 and caused to enter into the inlet end of a distributor pipe 58 extending horizontally within the vessel 14 above the fire tube 55, and discharged from said distributor pipe adjacent the head 15.

The dilute desiccant is thus delivered into the heating zone of the reconcentrator and therein elevated to a temperature suflicient tovaporize most of the water therefrom. This water, as steam, passes from the vessel 14 through an opening 59 into the lower end' of the column 45 and flows upwardly through said column counter-currently to the downwardly moving dilute desiccant. In addition to reflux and condensation due to cooling by heat exchange with the incoming dilute desiccant, the steam and vapors passing upwardly through the column are also subjected to atmospheric cooling, especially in an aircooled multiple tube section so at the uppermost end of the column 45, and effective rectification of the desiccant into concentrated, substantially water-free desiccant, and Water vapor is achieved.

The hot reconcentrated desiccant spills over the upper edge of the weir 56 into contact with the head 13, and accumulates in the space between the weir 56 and said head. Because the vessel 11 and the head 13 thereof are constructed of relatively thick metal, a heavy metallic flow path for the transmission of heat is provided, and quite appreciable quantities of heat are extracted from the hot desiccant to flow through this metallic path for transfer to the water accumulating in the separator sec tion A between the head 13 and the bafile 20. Not only is the desiccant thus relieved of considerable quantities of its heat, but warming of the water separated from the well stream is obtained to prevent freezing thereof. Also, heat is imparted to the oil or distillate separated from the well stream and the solidification therein of gums or the formation of stable emulsions, is minimized. As previously noted, the reconcentrated, and somewhat cooled, desiccant is discharged from the space between the weir 56 and the partition 13 through the outlet fitting 46.

Because of the relative coolness of the head 13, there may be some tendency for water vapor or steam generated in the heating of the dilute desiccant to pass over the uppcr edge of the weir 56 and condense upon the upper portion of the head 13. For this reason, there is provided 0. depending battle 61 extending downwardly from the upper wall of the vessel 14 between the weir 56 and the head 13 and projecting below the liquid level of reconcentrated desiccant present in the lower portion of this space. The bafile 61 may be positioned closely adjacent the head 13, but so long as it is not in contact with the head 13. it encloses with the head a dead gas space which functions as an insulator and prevents such condensation of water vapor or steam. Of course, if this condensation were permitted to occur, the water would drop directly into the reconcentrated desiccant and undesirably dilute the same.

i noted hereinberore, the dilute desiccant is drained dehydrator chamber C into a volume tank 37 neat-controlled discharge to the reconcentrator section B. T he Water and distillate separated in the separator section and discharged therefrom through the water leg 2.2 and distillate outlet 23 are similarly conducted into volume tanks 62 and 63, respectively, which are substantiaily identical in all respects to the volume tank 37. The structure of these volume tanks is shown in Fig. 12, the tructure comprising a short, cylindrical, horizontal vessel a} having one end closed by a domed or dished head 65,

to the other end provided with a flange fitting 66 carry- .a external pilot valve mechanism 6'7 and an internal supported upon an arm 69 extending to the pilot valve structure 67. An inlet fitting 74 is provided in the top wall of the vessel 64 for connection respectively to the discharge fittings 22, 23 or 29, and likewise, a discharge or outlet fitting 71 is provided in the bottom of the volume tanks for connection, in the case of the desiccant tank to the conductor 33, and in the case of the water and distillate discharges to conductors 72 and 73, respectively, leading to diaphragm valves 74 and 75, interposed, in turn, in a water outlet conductor '76 leading to a point of water disposal, and a distillate outlet conductor 77 leading to suitable storage facilities.

the operation of these volume tanks, the diaphragm valves remain closed until sufiicient liquid has accumulated in the volume tanks to lift the float 68 and through the pilot valve 67 actuate said diaphragm valves to open the same and discharge liquid from the volume tank.

A supply of gas at various pressures is needed for the operation of the diaphragm discharge valves, for the driving of the pump 50, and for firing of the burner or heating unit 55. With these purposes, gas is withdrawn from the gas discharge outlet fitting 36 through a branch conductor 78 leading through a pressure reducing regulator 79 to a gas supply manifold 80. From the manifold 80, gas is taken ofi through a pipe 81 for supplying the pump 50 and through an elongate pipe 82, extending substantially the full length of the unit for supply through a main burner pipe 83 to the burner of the heating unit 55 and through a branch pipe 84 to the pilot light of such burner.

A supply of gas is also taken off from the manifold at reduced pressure through a regulator 85 and thence through a conductor 86 to a pilot gas manifold jacket 87 which surrounds the elongate pipe 82 and is in heat exchange relationship therewith. Gas undergoes a drop in temperature when it is subjected to a pressure reduction, and in some instances, freezing of the moisture in the gas may occur. The pressure reduction in the regulator 79 is not sufficient, normally, to create a freezing problem, but the further reduction through the regulator 85 may cause sufiicient loss of temperature as to pose a problem in cold Weather or cold climates. Hence, the conduction of the pilot gas into the heat exchange jacket 87 makes provision for rewarming of the pilot gas supply after it has undergone pressure reduction and temperature drop in the regulator 85'. As shown in Fig. 9, pilot gas is taken from the manifold 87 through supply pipes 88 to the pilot valve structures 67 of the water and oil discharges, and selectively admitted by the pilot valve structure to the diaphragm valves 74 and 75 for operation thereof. A supply of pilot gas is also taken from the manifold jacket through a conductor 89 to a thermostat control device 99 projecting into the heating chamber of the reconcentrator section B, and controlled by said thermostat device to operate a diaphragm valve 91 which regulates the supply of fuel gas to the main burner of the heating unit 55. Pilot gas for the diaphragm 39 of the desiccant discharge structure may be taken from the jacket 87, or may be taken directly from the pipe 86 through the conductor 2 to the pilot valve structure 67 of the desiccant discharge volume tank 37 and passed therefrom through the conductor 93 to the diaphragm valve 39.

It will be seen from the foregoing that adequate provision has been made for protecting the pilot gas supply against freezing resulting from pressure reduction.

The combining of the desiccant reconcentrator and the well stream separator into a single vessel also makes possible the provision of a further safeguard against freezing or congealing of liquids in the separator section as well as the protection of much of the operating equipment from cold weather or cold climates. Desirably, the legs or supports 16 for the composite vessel 10 are carried upon elongate horizontal skids or support members 94 joined by transverse members 95. The pump 50 and all other accessories and appurtenances of the unit are connected to and supported upon either the skids 94 or the tank unit it and thus, the entire structure is assembled into a compact unitary separating and dehydrating device. Such structure facilitates transportation and moving of the unit as well as its positioning in the field and connection to various supply and discharge conductors or pipes.

There is a further and very important advantage, however, in the incorporation of an enclosure housing having its bottom 96 extending between the skids 94, its transverse end walls 97 extending between each pair of the supports 16, its sidewalls 98 extending lengthwise of the unit between the supports 16, and an inclined top or roof section 99 merging into the side walls of the vessel 10. A quite appreciable portion of the lower part of the reconcentrator section B is thus exposed to the interior of the housing or enclosure 100 constituted by the enumerated walls, and the lower portion of the separator section A, within which normally-freezable liquids are accumulated, is also exposed to this warm interior of the housing. Thus, a further and very elfective safeguard against freezing of these liquids is provided, and at the same time, an enclosure is provided for many of the pipes, conductors, fittings and appurtenances of the unit. Obviously, the housing 100 may be insulated to enhance the retention of heat therein.

A modified form of the invention is shown in Fig. 4 in which provision is made in the separator section only for the removal of liquids and not for the resolving of the separated liquids into distillate and water components. This structure is substantially identical to that as previously described, and the same numerals, where applicable, have been used throughout. In the modification, the bafile 20 and the water leg 22 are omitted, and all liquids are discharged through the single outlet 23. There is provided within the vessel 11 between the inlet box 18 and the outlet 23 a liquid separating and mist extracting unit 101 comprising a plurality of closely spaced plates 102 extending transversely of the separator enclosure and disposed at an angle with respect to the horizontal. These plates provide a multiplicity of surfaces upon which liquid droplets and particles may settle from the gas stream passing therebetween and greatly reduce the vertical distance through which such droplets or particles must descend before encountering a surface which they can wet and to which they will adhere or cling. The accumulated liquids drain downwardly over the surfaces of the plate and accumulate in the lower portion of the separator section between the head 13 and the partition 21.

For control of liquid discharge through the outlet fitting 23, the volume tank 63 is omitted, and instead, a flange fitting 103 is provided in the side Wall of the vessel 11 adjacent the outlet 23 for the reception and support of a liquid level float 104 operating a pilot valve mechanism 105. The diaphragm valve 75 is retained and connected into the discharge outlet conductor 23, the valve being actuated or operated by means of the pilot valve controller 105 rather than the controller 67 of the volume tank 63. The dilute glycol is discharged from the dehydrator section C through the outlet fitting 29 into the volume tank 37 as shown in Fig. 9.

In operation, this modification of the invention functions substantially identically to the previously described form, the only difference being the discharge of commingled distillate and water from the separator section through the outlet 23 rather than the separate discharge of water and liquid through the outlets 22 and 23.

A still further modification of the invention is shown in Figs. 13 through 17. This form of the invention is quite similar in most respects to that shown in Fig. 4, the principal changes being in the location of the heat exchanger coil 52, the heat exchanger 42 connected to the reconcentrated glycol outlet 46, the structure of the bubble column of the desiccant reconcentrator, and the arrangement of the auxiliary supply piping.

As shown in Fig. 13, the heat exchange coil 52, mist eliminator 35 and gas outlet fitting 36 of the first described forms of the invention are eliminated from the interior of the vessel 11, and an upright cylindrical dome or tower 106 is positioned in the upper wall of the vessel 11 so as to extend upwardly from the upper wall thereof adjacent the head 12. The upper end of the dome 106 is closed by a domed head 107 having therein a gas outlet fitting 108, while the bottom of the dome is open to the interior of the vessel 11. A maze or mist extractor 109 extends transversely across the lower portion of the dome 106, and a helical heat exchange coil 110 is disposed in the dome above the mist extractor and surrounding a closed top drum 111 supported from the inner wall of the dome by suitable spaced brackets 112. Thus, gas leaving the vessel 11 is caused to flow upwardly from the mist extractor 109 and then through the annular space between the drum 111 and the inner wall of the dome 106 in close thermal contact with the coil 110 before exiting from the outlet fitting 108. More complete and efiicient contact and heat exchange relationship between the outwardly flowing gas and the heat exchange coil is thus assured, and a somewhat enlarged vertical flow space is provided for a maximum removal of liquid particles from the gas stream.

This structure also eliminates the need for the desiccant volume tank 37, the dilute desiccant flowing from the outlet fitting 29 directly to the diaphragm valve 39, the latter, in turn, being controlled in the manner common in this art by a float 113 disposed within the vessel 11 between the bafile 27 and the head 12 and actuating a pilot valve mechanism 114 mounted in a collar 115 extending laterally from the vessel 111 with its axis positioned in a horizontal plane extending through the axis of the vessel 11.

The heat exchanger 42 is also eliminated and replaced by an enlarged cylindrical sump 116 depending from the vessel 14 of the reconcentrator section 13 between the battle 56 and the head 13. A reconcentrated desiccant outlet 117 is provided in the bottom of the sump 116, and a helical heat exchange coil 118 is positioned within the sump with a dilute desiccant inlet 119 projecting through the wall of the sump. The outlet of the heat exchange coil extends upwardly through the vessel 14 to a preheated, dilute desiccant outlet fitting 120 in the upper wall of the vessel 14, from which the preheated dilute desiccant passes to the bubble column of the reconcentrator. The addition of the sump 116 enlarges the internal volume of the reconcentrator section and provides a surge space or volume for the reconcentrated desiccant.

The bubble column of the reconcentrator is modified to the extent of being provided with a distillate skimmer drum 121 surrounding the upper portion column 45 immediately below the tube bundle 60'. The preheated, dilute desiccant flows from the outlet fitting 120 of the heat exchange coil 118 through a conductor 122 to the inlet fitting 123 of the drum 121 at which point the desiccant is permitted to flow into the relatively large interior of the drum 121 and to stratify therein in surrounding heat exchange relationship with the upper portion of the bubble column 45. Any distillate or hydro carbon present in the desiccant will separate therefrom and stratify into an upper layer which is drawn oil through the distillate outlet 124 in the upper side wall of the drum 121, while the desiccant flows under a transverse bafile 125 provided interiorly of the drum 121 and into a desiccant outlet conductor 126 to flow downwardly and enter the column 45' through the inlet fitting 127. In this manner, distillate is prevented from entering into the heating chamber of the reconcentrator and therein constituting a fire hazard and an impediment to effective reconcentration of the desiccant, and also such quantities of distillate as may be recovered in this fashion, are conserved and protected against loss.

With the exception of the auxiliary gas flow, the operation of this modification is substantially the same as that previously described, the desiccant, of course, being passed through the heat exchanger 110 rather than the heat exchanger 52 prior to its introduction into the dehydrator section C by means of the inlet fitting 24. Further the dilute desiccant is passed through the heat exchanger 118 rather than through the heat exchanger 42. Otherwise, the flow of the various fluids is the same as that previously described.

For providing an auxiliary gas supply, the dome 106 is provided with an auxiliary gas outlet 128 in its side wall above the mist extractor 109, and the auxiliary gas is taken from this outlet through a pipe 129 to a pressure reducing regulator 130 and thence by a pipe 131 through an oil lubricator 132 to the motive gas inlet of a gas driven pump 133. The exhaust motive gas flows from the pump through a conductor 134 into a gas manifold 135 whereby the gas employed for driving the pump 133 is conserved. The main burner and pilot burner gas supply for the heating unit of the reconcentrator section is taken ofi from the manifold 135 through the pipe 82, as previously described, and pilot gas for the operation of the diaphragm valves 39 and 75 is similarly drawn ofi from the manifold. To provide for the contingency of a greater gas demand from the manifold 35 than will pass thereto through the gas driven pump 133, a by-pass conductor 136 is connected between the pipe 131 and the manifold through a pressure reducing regulator 137. Further, to provide for accumulation of gas or excessive pressure in the manifold 135, the latter is provided with an excess pressure relief valve 138 leading to a flare or other point of gas disposal.

This form of the invention also may have the major portion of its lower section enclosed in a housing extending from the combination separator and desiccant reconcentrator vessel downwardly to the skids 94 and having its ends defined by the legs 16' upon which the vessel is supported upon the skids. This housing 139 is shown partially broken away in Fig. 13 of the drawmgs.

In all of the forms of the invention, the reconcentrator and separator section are incorporated into a single vessel whereby heat exchange through the common head or partition 13 is afforded, as well as a metallic path for the flow of heat through the walls of the vessels 11 and 14. In this manner, desirable quantities of heat are removed from the reconcentrated desiccant and transferred to the separated layers of liquid in the separator section A in order to prevent freezing or congealing of such liquids therein. In addition, a major portion of the piping and appurtenances of the unit are enclosed within a housing to which heat is supplied interiorly from the reconcentrator section, and protection against cold weather or cold climates is afforded thereto.

The foregoing description of the invention is explanatory thereof and various changes in the size, shape and materials, as well as in the details of the illustrated con struction may be made, within the scope of the appended claims, without departing from the spirit of the invention.

What I claim and desire to secure by Letters Patent is:

1. A combination liquid-gas separator and gas dehydrator for petroleum well streams including, a unitary elongate horizontal vessel, a transverse vertical partition in the vessel dividing said vessel into a separator section and a reconcentrator section having the partition as a wall in common, a well stream inlet to the separator sec tion, means for discharging liquids from the separator section, a gas outlet from the separator section, a liquid desiccant inlet to the separator section, means in the separator section for separating the liquid and gaseous phases of the well stream, means in the separator section for passing the separater gaseous phase in contact with the liquid desiccant to dehydrate the gaseous phase, heating means in the reconcentrator section, water vapor discharge means in the reconcentrator section, means for admitting dilute desiccant to the reconcentrator section and delivering reconcentrated desiccant therefrom, means for circulating dilute desiccant from the separator section to the reconcentrated section and for circulating reconcentrated desiccant from the reconcentrator section to the separator section, the reconcentrator section having a reconcentrateddesiccant accumulation chamber adjoining the vertical partition with the partition forming one wall of the chamber, and a bafile depending from the top wall of the reconcentrator section into the chamber closely adjacent the partition.

2. A combination liquid-gas separator and gas dehydrator for petroleum well streams including, a unitary elongate horizontal vessel, a transverse vertical partition in the vessel dividing said vessel into a separator section and a reconcentrator section having the partition as a wall in common, a well stream inlet to the separator section, means for discharging liquids from the separator section, a gas outletfrom the separator section, a liquid desiccant inlet to the separator section, means in the separator section for separating the liquid and gaseous phases of the well stream, means in the separator section for passing the separated gaseous phase in contact with the liquid desiccant to dehydrate the gaseous phase, heating means in the reconcentrator section, water vapor discharge means in the reconcentrator section, means for admitting dilute desiccant to the reconcentrator section and delivering reconcentrated desiccant therefrom, and means for circulating dilute desiccant from the separator section to the reconcentrated section and for circulating reconcentrated desiccant from the reconcentrator section to the separator section, the reconcentrator section having a reconcentrated-desiccant accumulation chamber adjoining the vertical partition with the partition forming one wall of the chamber, and the separator section having a separated liquids accumulation zone closely adjacent the vertical partition.

3. A combination liquid-gas separator and gas dehydrator for petroleum well streams including, a unitary elongate horizontal vessel, a transverse vertical partition in the vessel dividing said vessel into a separator section and a reconcentrator section having the partition as a wall in common, a Well stream inlet to the separator section, means for discharging liquids from the separator section, a gas outlet from the separator section, a liquid desiccant inlet to the separator section, means in the separator section for separating the liquid and gaseous phases of the well stream, means in the separator section for passing the separated gaseous phase in contact with the liquid desiccant to dehydrate the gaseous phase, heating means in the reconcentrator section, water vapor discharge means in the reconcentrator section, means for admitting dilute desiccant to the reconcentrator section and delivering reconcentrated desiccant therefrom, and means for circulating dilute desiccant from the separator section to the reconcentrated section and for circulating reconcentrated desiccant from the reconcentrator section to the separator section, the reconcentrator section having a reconcentrated-desiccant accumulation chamber adjoining the vertical partition with the partition forming one wall of the chamber, and the separator section having a separated liquids accumulation chamber adjoining the vertical partition with said partition forming one wall of the liquids accumulation chamber.

4. A combination liquid-gas separator and gas dehydrator for petroleum well streams including, a unitary vessel having an intermediate partition dividing the vessel into a separator section and a reconcentrator section, a well stream inlet to the separator section, means for discharging liquids from the separator section, a gas outlet from the separator section, a liquid desiccant inlet to the separator section, means in the separator Section for separating the liquid and gaseous phases of the well stream, the separator section having a separated liquids accumulation chamber in its lower portion adjacent the intermediate partition, means in the separator section for passing the separated gaseous phase in contact with the liquid desiccant to dehydrate the gaseous phase, heating means in the reconcentrator section, water vapor discharge means in the reconcentrator section, means in the reconcentrator section for retaining a heated body of desiccant in proximity to the heating means and exposed to the lower portion of the reconcentrator section, means for admitting dilute desiccant to the reconcentrator section and delivering reconcentrated desiccant therefrom, and means for circulating dilute desiccant from the separator section to the reconcentrator section and for circulating reconcentrated desiccant from the reconcentrator section to the separator section, and an insulating housing enclosing in common the lower portion of the separator section containing the separated liquids accumulation chamber and the lower portion of the reconcentrator section exposed to the body of heated desiccant.

5. A combination unit as set forth in claim 3, and an insulating housing enclosing in common the lower pot tions of the vessel containing the reconcentrated desiccant References Cited in the file of this patent UNITED STATES PATENTS Raigorodsky Sept. 10, 1940 

1. A COMBINATION LIQUID-GAS SEPARATOR AND GAS DEHYDRATOR FOR PETROLEUM WELL STREAMS INCLUDING, A UNITARY ELONGATE HORIZONTAL VESSEL, A TRANSVERSE VERTICAL PARTITION IN THE VESSEL DIVIDING SAID VESSEL INTO A SEPARATOR SECTION AND A RECONCENTRATOR SECTION HAVING THE PARTITION AS A WALL IN COMMON, A WELL STREAM INLET TO THE SEPARATOR SECTION, MEANS FOR DISCHARGING LIQUIDS FROM THE SEPARATOR SECTION, A GAS OUTLET FROM THE SEPARATOR SECTION, A LIQUID DESICCANT INLET TO THE SEPARATOR SECTION, MEANS IN THE SEPARATOR SECTION FOR SEPARATING THE LIQUID AND GASEOUS PHASES OF THE WELL STREAM, MEANS IN THE SEPARATOR SECTION FOR PASSING THE SEPARATER GASEOUS PHASE IN CONTACT WITH THE LIQUID DESICCANT TO DEHYDRATE THE GASEOUS PHASE, HEATING MEANS IN THE RECONCENTRATOR SECTION, WATER VAPOR DISCHARGE MEANS IN THE RECONCENTRATOR SECTION, MEANS FOR ADMITTING DILUTE DESICCANT TO THE RECONCENTRATOR SECTION AND DELIVERING RECONCENTRATED DESICCANT THEREFROM, MEANS FOR CIRCULATING DILUTE DESICCANT FROM THE SEPARATOR SECTION TO THE RECONCENTRATED SECTION AND FOR CIRCULATING RECONCENTRATED DESICCANT FROM THE RECONCENTRATOR SECTION TO THE SEPARATOR SECTION, THE RECONCENTRATOR SECTION HAVING A RECONCENTRATEDDESICCANT ACCUMULATION CHAMBER ADJOINING THE VERTICAL PARTITION WITH THE PARTITION FORMING ONE WALL OF THE CHAMBER, AND A BAFFLE DEPENDING FROM THE TOP WALL OF THE RECONCENTRATOR SECTION INTO THE CHAMBER CLOSELY ADJACENT THE PARTITION. 